EP0488182A2 - Verfahren zur Herstellung von Polycarbonat - Google Patents

Verfahren zur Herstellung von Polycarbonat Download PDF

Info

Publication number
EP0488182A2
EP0488182A2 EP91120202A EP91120202A EP0488182A2 EP 0488182 A2 EP0488182 A2 EP 0488182A2 EP 91120202 A EP91120202 A EP 91120202A EP 91120202 A EP91120202 A EP 91120202A EP 0488182 A2 EP0488182 A2 EP 0488182A2
Authority
EP
European Patent Office
Prior art keywords
carbonates
dihydroxy compounds
amount
compounds
inert solvent
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
EP91120202A
Other languages
English (en)
French (fr)
Other versions
EP0488182A3 (en
Inventor
Kouichi c/o Idemitsu Petrochemical Kurosawa
Shigeki c/o Idemitsu Petrochemical Kuze
Noriyuki C/O Idemitsu Petrochemical Kunishi
Masaya c/o Idemitsu Petrochemical Okamoto
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Idemitsu Petrochemical Co Ltd
Original Assignee
Idemitsu Petrochemical Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Idemitsu Petrochemical Co Ltd filed Critical Idemitsu Petrochemical Co Ltd
Publication of EP0488182A2 publication Critical patent/EP0488182A2/de
Publication of EP0488182A3 publication Critical patent/EP0488182A3/en
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G64/00—Macromolecular compounds obtained by reactions forming a carbonic ester link in the main chain of the macromolecule
    • C08G64/20—General preparatory processes
    • C08G64/30—General preparatory processes using carbonates

Definitions

  • the present invention relates to a process for producing a polycarbonate. More particularly, it relates to a process for efficiently producing a polycarbonate which is excellent in color tone, heat resistance and water resistance.
  • PC polycarbonate
  • the interfacial polycondensation method and the transesterification method are often employed.
  • Each of these methods has its advantages, but, on the contrary, has various disadvantages.
  • the interfacial polycondensation method can produce a high quality PC, but requires a large equipment in processing, which comes to cost much.
  • the transesterification method had various disadvantages. Since the reaction is effected at high temperature, branching or crosslinking is easily caused, and accordingly high quality polymer is hardly produced. Moreover, coloration is unavoidable because of the reaction at high temperature for a long period (see Mikio Matsukane et al., Plastic Material Series [5] "Polycarbonate Resin” by Nikkan Kogyo Shimbunsha, 1969, pp.62-67).
  • the present inventors have intensively studied to improve color tone, heat resistance and water resistance in PC, and to develop a process for efficiently producing PC with high quality.
  • the present invention provides a process for producing polycarbonate, which comprises transesterifying
  • the aromatic dihydroxy compounds to be used in the present invention vary in kind.
  • Example of said compounds are those represented by the formula (I): wherein X is -S-, -SO- or SO2-, R1 and R2 are each a hydrogen atom or monovalent hydrocarbon group, R3 is a divalent hydrocarbon group, R4 and R5 are each a hydrogen atom, a monovalent hydrocarbon group or a halogen atom, and m and n indicates an integer of 1 to 4.
  • bis(hydroxyaryl)alkanes such as bis(4-hydroxyphenyl)methane, 1,1-bis(4-hydroxyphenyl)ethane, 2,2-bis(4-hydroxyphenyl)propane (common name: bisphenol A), 2,2-bis(4-hydroxyphenyl)butane, 2,2-bis(4-hydroxyphenyl)octane, 2,2-bis(4-hydroxyphenyl)phenyl methane, 2,2-bis(4-hydroxy-1-methylphenyl)propane, 1,1-bis(4-hydroxy-t-butylphenyl)propane, 2,2-bis(4-hydroxy-3-bromophenyl)propane, 2,2-bis(4-hydroxy-3,5-tetramethylphenyl)propane, 2,2-bis(4-hydroxy-3-chlorophenyl)propane, 2,2-bis(4-hydroxy-3,5-tetrachlorophenyl)propane, and 2,2-bis(4-(4-hydroxyphen
  • various aliphatic dihydroxy compounds can be used in the present invention.
  • specific examples of said compounds are butane-1,4-diol, 2,2-dimethylpropane-1,3-diol, hexane-1,6-diol, diethyleneglycol, triethyleneglycol, tetraethyleneglycol, octaethyleneglycol, dipropyleneglycol, N,N-methyldiethanolamine, cyclohexane-1,3-diol, cyclohexane-1,4-diol, 1,4-dimethylolcyclohexane, p-xylileneglycol, 2,2-bis-(4-hydroxycyclohexyl)-propane, and products of ethoxication or propoxication of dihydric alcohol or phenol, such as bis-oxyethyl-bisphenol A, bis-oxyethyl-tetrachlorobisphenol A and bis-oxye
  • bisesters of aromatic dihydroxy compounds bisesters of aliphatic dihydroxy compounds, carbonates of aromatic dihydroxy compounds, or carbonates of aliphatic dihydroxy compounds to be used in the present invention
  • bisesters ((II) or (IV)) or carbonates ((III) or (V)) of the above compounds are mentioned.
  • R indicates the residue after two hydroxyl groups are removed from the above-mentioned aliphatic dihydroxy compound
  • Ar1 indicates the residue after two hydroxyl groups are removed from the above-mentioned aromatic dihydroxy compounds
  • R6 indicates an alkyl group having 1 to 6 carbon atoms or a cycloalkyl group having 4 to 7 carbon atoms.
  • Material (B) to be used in the present invention is a diaryl carbonate, a dialkyl carbonate, or an alkylaryl carbonate.
  • favourable diaryl carbonates, dialkyl carbonates, and alkylaryl carbonates are those represented by the formulae (VI), (VII), and (VIII), respectively: wherein R6 is as defined above, and Ar2 indicates an aryl group.
  • the process of the present invention employs above-mentioned materials (A) and (B), which must be reacted in an inert solvent.
  • the inert solvent to be used therein can be selected properly according to the circumstances.
  • aromatic compounds such as diphenylether, halogenated diphenylether, diphenylsulfone, benzophenone, polyphenylether, dichlorobenzene, and methylnaphthalene; gases such as carbon dioxide, nitrogen, dinitrogen oxide and chlorofluorohydrocarbon; alkanes such as ethane, and propane; cycloalkanes such as cyclohexane, tricyclo(5,2,10)-decane, cyclooctane, and cyclododecane; alkenes such as ethene and propene; and sulfur hexafluoride.
  • diphenylether is particularly favorable.
  • terminators shown below can be used, though they are not defined in the present invention.
  • Specific examples of such terminators are monohydric phenols such as o-n-butylphenol, m-n-butylphenol, p-n-butylphenol, o-isobutylphenol, m-isobutylphenol, p-isobutylphenol, o-t-butylphenol, m-t-butylphenol, p-t-butylphenol, o-n-pentylphenol, m-n-pentylphenol, p-n-pentylphenol, o-n-hexylphenol, m-n-hexylphenol, p-n-hexylphenol, o-cyclohexylphenol, m-cyclohexylphenol, p-cyclohexylphenol, o-phenylphenol, m-phenylphenol, p-phenylphenol, o-n-n
  • p-t-butylphenol p-cumylphenol
  • p-phenylphenol are preferred, though they are not specified in the present invention.
  • carbonic acid diesters are used in some cases.
  • Specific examples of terminators of these carbonic acid diesters are carbobutoxyphenylphenylcarbonate, methylphenylbutylphenylcarbonate, ethylphenylbutylphenylcarbonate, dibutyldiphenylcarbonate, biphenylphenylcarbonate, dibiphenylcarbonate, cumylphenylphenylcarbonate, dicumylphenylcarbonate, naphthylphenylphenylcarbonate, dinaphthylphenylcarbonate, carbopropoxyphenylphenylcarbonate, carboheptoxyphenylphenylcarbonate, carbomethoxy-t-butylphenylphenylcarbonate, carboprotoxyphenylmethylphenylphenylcarbonate, cromanylphenylcarbonate, and dicromanylcarbonate.
  • the amount of terminators such as monohydric phenols and carbonic acid diesters as above is in the range of 0.05 mol% to 10 mol% to 1 mol of dihydroxy compound as material (A), the ends of hydroxyl group of the resulting polycarbonate are sealed, and a polycarbonate which is sufficiently excellent in heat resistance and water resistance is obtained and the rate of polymerization and condensation becomes favorably higher.
  • These monohydric phenols or carbonic acid diesters may be added in the whole amount in advance to the reaction system, or they may be added partly in advance, and the residue may be added according as the reaction proceeds. Further, in some cases, they may be added to the reaction system at once, after the polycondensation reaction of dihydroxy compound of above-mentioned material (A) and the carbonate of material (B) partly proceeds.
  • the present invention requires no catalyst, but known catalysts may be used to promote the transesterification.
  • these catalysts are single substances, oxides, hydroxides, amides, alcoholates, and phenolates of alkali metals or alkali earth metals; basic metal oxides such as ZnO, PbO, and Sb2O3, organic titanium compounds, soluble manganese compounds, acetates of Ca, Mg, Zn, Pb, Sn, Mn, Cd, and Co; combined catalysts such as nitrogen-containing basic compound and boron compound, nitrogen-containing basic compound and alkali (earth) metal compound, nitrogen-containing basic compound, alkali (earth) metal compound and boron compound.
  • the process of the present invention is to produce PC in the presence of an inert solvent. More specifically, the reaction proceeds according to the conventional transesterification method. The procedure and conditions of the process of the present invention are shown specifically as follows.
  • the amount of material (A), dihydroxy compounds such as aromatic dihydroxy compounds, aliphatic dihydroxy compounds, bisesters of aromatic dihydroxy compounds, carbonates of aromatic dihydroxy compounds, bisesters of aliphatic dihydroxy compounds, or carbonates of aliphatic dihydroxy compounds and the amount of material (B), carbonates such as diaryl carbonates, dialkyl carbonates or alkylaryl carbonates are adjusted so that the ratio of the amount of (B) to the amount of (A) is 1 to 1.5 times mol. According to the circumstances, the amount of the carbonates is preferred to be 1.02 to 1.20 times mol, which is somewhat in excess of the amount of dihydroxy compounds.
  • the reaction temperature is not critical, but usually it is in the range of 100°C to 330°C, preferably 180°C to 300°C. It is more preferred to gradually raise the temperature from 180°C to 300°C according as the reaction proceeds. Reactions proceed slowly under 100°C, while over 330°C the resultant polymer is unfavorably deteriorated by heat.
  • the pressure at reaction can be set depending on the reaction temperature in accordance with the steam pressure of the monomer to be used. It is set so that the reaction goes efficiently, and not to be restricted. Usually at the initial stage of reaction, the pressure is set under 1 to 50 atm (760 to 38000 torr), and at the latter stage of reaction, the pressure is often reduced, favorably to be 0.01 to 100 torr finally.
  • the reaction may be continued until the desired molecular weight is obtained, so the reaction time is usually 0.2 to 10 hours.
  • reaction is conducted in the presence of an inert solvent in an amount of 1 to 60% by weight, favorably 5 to 40% by weight based on the total of the theoretical amount of PC produced from the before-mentioned materials (A) and (B), and the amount of the inert solvent, according as the reaction proceeds.
  • the way of supplying the materials for said reaction is not limited particularly, and any step may be taken.
  • Said inert solvent is used by the reasons (i) to (iii) as follows.
  • Said inert solvent exhibits no effect when used in an amount under 1% by weight of the before-mentioned theoretical amount of resulting PC.
  • the amount of said solvent is in excess of 60% by weight, the viscosity of the reaction mixture is lowered, but there involved the problems in that the molecular weight of the resulting PC does not increase in a short time since monomers come more rarely in contact with each other, and that an enormous cost is required for recovering the solvent.
  • phenols, alcohols or esters thereof corresponding to the carbonates used as the starting material, and inert solvent are released from the reactor. These released materials can be separated and purified to be recycled, and equipments to remove them is desired, if possible.
  • the process of the present invention can be conducted batchwise or continuously, and any equipment can be used in this process. In a continuous production, it is preferred to use at least two reactors to set the reaction conditions as above.
  • reactors are not critical, so long as it posseses an ordinary stirring function. However, as the viscosity is raised at the latter stage of the reaction, reactors are preferred to have a stirring function for high viscosity. Further, the shape of the reactor may be extruder type as well as tank type.
  • antioxidants can be used, if necessary.
  • phosphoric antioxidant agents such as tris(nonylphenyl)phosphite, trisphenylphosphite, 2-ethylhexyldiphenylphosphite, trimethylphosphite, triethylphosphite, tricresylphosphite, and triarylphoshite can be used.
  • PC obtained in the above manner may be pelletized directly, or can be molded by the use of an extruder or the like.
  • PC obtained by the present invention can be used with conventional additives such as plasticizer, pigment, lubricant, mold-releasing agent, stabilizer, inorganic filler and the like.
  • said PC can be used in mixtures with polymers such as polyester, polysulfonate, polyamide, polyphenyleneoxide and the like.
  • the use of a specified amount of inert solvent lowers the viscosity of the system, and shorten the reaction time, thus, a PC which is excellent in color tone (transparency), heat resistance, and water resistance can be efficiently produced.
  • the present invention can be utilized effectively and widely as a process for producing a high quality PC advantageously on an industrial scale.
  • the reaction was conducted with stirring for one hour, while the pressure was kept finally at 0.5 torr, and a viscous transparent polycondensate, that is, PC remained lastly in the autoclave.
  • the PC was dissolved in methylene chloride, and measured for viscosity average molecular weight to obtain the value of 22000.
  • the resulting PC was pulverized, and put in an extruder at 220 to 270°C to be pelletized. Said pellet was injection molded, and the resulting molding was tested for YI and hot water tension. The result is shown in Table 1.
  • Example 1 The procedure of Example 1 was repeated except that kind of monomer, amount of diphenylether, and reaction time varied in each Example.
  • the resulting PCs were pulverized, put in the extruder at 220 to 270°C to be pelletized.
  • the pellet was injection molded and tested for YI and hot water tension. The result is shown in Table 1.
  • Example 1 The procedure of Example 1 was repeated except that 228 g (1 mol) of bisphenol A, 257 g (1.2 mol) of diphenyl carbonate and 28.2 g (0.17 mol, 10% by weight) of diphenyl ether, and 6.8 g (0.05 mol to the amount of bisphenol A) of p-cumylphenol as the terminator were placed.
  • PC that is, a viscous and transparent polycondensate which remained in the autoclave lastly was dissolved in methylene chloride, and measured for the viscosity average molecular weight, to obtain the value of 20500.
  • the result of hot water tension test showed that a resin excellent in water resistance could be obtained.
  • the resulting PC was pulverized to be pelletized at 220 to 270°C by an extruder. The pellet was injection molded, and subjected to YI and hot water tension test. The result is shown in Table 1.
  • Example 1 The procedure of Example 1 was repeated except that 228 g (1 mol) of bisphenol A, 257 g (1.2 mol) of diphenyl carbonate and 28.2 g (0.17 mol, 10% by weight) of diphenylether, and, as the catalysts, 0.018 g of boric acid, 0.18 g of 15% aqueous solution of tetramethylammoniumhydroxide, and 0.003 g of sodium hydrogencarbonate were placed.
  • PC the viscous and transparent condensate which remained in the autoclave lastly was dissolved into methylene chloride, and measured for the viscosity average molecular weight to obtain a value of 24000.
  • the resulting PC was pulverized to be pelletized at 220 to 270°C by an extruder. The pellet was injection molded, and subjected to YI test and hot water tension test. The result was shown in Table 1.
  • Example 8 The procedure of Example 8 was repeated except that diphenylether was not used.
  • the resulting PC was pulverized to pelletized at 220 to 270°C by an extruder.
  • the pellet was injection molded, and subjected to YI test and hot water tension test. The result is shown in Table 1.
  • Example 1 The procedure of Example 1 was repeated except that 228 g (1 mol) of bisphenol A, 257 g (1.2 mol) of diphenyl carbonate and 28.2 g (0.15 mol, 10% by weight) of benzophenone were placed.
  • PC the viscous and transparent condensate which remained in the autoclave lastly was dissolved into methylene chloride, and measured for the viscosity average molecular weight to obtain a value of 19000.
  • the resulting PC was pulverized, and pelletized at 220 to 270°C by an extruder. The pellet was injection molded, and subjected to YI test and the hot water tension test. The result is shown in Table 1.
  • Example 1 The procedure of Example 1 was repeated except that 228 g (1 mol) of bisphenol A, 257 g (1.2 mol) of diphenyl carbonate, and 28.2 g (0.20 mol, 10% by weight) of 1-methylnaphthalene were placed.
  • PC the viscous and transparent polycondensate lastly remained in the autoclave was dissolved in methylene chloride, and measured for the viscosity average molecular weight, to obtain the value of 16300.
  • the resulting PC was pulverized, and pelletized at 220 to 270°C by an extruduer. Said pellet was injection molded, and subjected to YI test and the hot water tension test. The result is shown in Table 1.
  • Example 1 The procedure of Example 1 was repeated except that 228 g (1 mol) of bisphenol A, 257 g (1.2 mol) of diphenyl carbonate, and 28.1 g (0.13 mol, 10% by weight) of diphenylsulfone were placed.
  • PC the viscous and transparent polycondensate lastly remained in the autoclave was dissolved in methylene chloride, and measured for the viscosity average molecular weight, to obtain the value of 17300.
  • the resulting PC was pulverized, and pelletized at 220 to 270°C by an extruder. The pellet was injection molded, and subjected to YI test and the hot water tension test. The result is shown in Table 1.
  • test piece As the hot water tension test, a test piece was dipped in hot water of 80°C for 16 hours, and then subjected to the tensile test (in accordance with JIS K7113-81) after 2 hours.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Polyesters Or Polycarbonates (AREA)
EP19910120202 1990-11-29 1991-11-26 Process for producing a polycarbonate Ceased EP0488182A3 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP325293/90 1990-11-29
JP2325293A JP2554775B2 (ja) 1990-11-29 1990-11-29 ポリカーボネートの製造方法

Publications (2)

Publication Number Publication Date
EP0488182A2 true EP0488182A2 (de) 1992-06-03
EP0488182A3 EP0488182A3 (en) 1993-01-13

Family

ID=18175198

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19910120202 Ceased EP0488182A3 (en) 1990-11-29 1991-11-26 Process for producing a polycarbonate

Country Status (3)

Country Link
US (1) US5322919A (de)
EP (1) EP0488182A3 (de)
JP (1) JP2554775B2 (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023118408A1 (en) 2021-12-24 2023-06-29 Avantium Knowledge Centre B.V. Process for the production of polyester copolymers

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR970702313A (ko) * 1994-04-08 1997-05-13 유미꾸라 레이이찌 말단 히드록실기를 갖는 폴리카르보네이트의 제조 방법(Process for Producing Hydroxyl-Terminated Polycarbonate)
JP4774610B2 (ja) * 2001-03-13 2011-09-14 三菱瓦斯化学株式会社 ポリカーボネートの製造方法
JP5589266B2 (ja) * 2008-06-09 2014-09-17 宇部興産株式会社 ポリ（アルキレンカーボネート）化合物の製造方法
DE102012105296A1 (de) * 2012-06-19 2013-12-19 Epc Engineering Consulting Gmbh Verfahren und Anlage zur Herstellung von Polycarbonat

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2439552A1 (de) * 1974-08-17 1976-02-26 Bayer Ag Verfahren zur herstellung von bisphenol-a-polycarbonat nach dem schmelzumesterungsverfahren
DE2523352A1 (de) * 1975-05-27 1976-12-09 Bayer Ag Verfahren zur herstellung aliphatischer polycarbonate
US4459384A (en) * 1981-11-09 1984-07-10 Union Carbide Corporation Process for preparing polyesters or poly(ester carbonates) in the presence of a processing aid
CA1214588A (en) * 1981-11-09 1986-11-25 Union Carbide Corporation Process for preparing polyesters or poly(estercarbonates) in the presence of a processing aid
JPS61151235A (ja) * 1984-12-24 1986-07-09 Nippon Polyurethan Kogyo Kk 脂肪族ポリカ−ポネ−トポリオ−ルの製造方法
SG73353A1 (en) * 1988-09-22 2000-06-20 Ge Plastics Japan Ltd Process for the production of polycarbonates
JPH02153927A (ja) * 1988-12-06 1990-06-13 Nippon G Ii Plast Kk ポリカーボネートの製造方法
JPH02153924A (ja) * 1988-12-06 1990-06-13 Nippon G Ii Plast Kk ポリカーボネートの製造方法
JP2628905B2 (ja) * 1988-12-06 1997-07-09 日本ジーイープラスチックス 株式会社 ポリカーボネートの製造方法
JPH02153926A (ja) * 1988-12-06 1990-06-13 Nippon G Ii Plast Kk ポリカーボネートの製造方法
JP2674813B2 (ja) * 1988-12-06 1997-11-12 日本ジーイープラスチックス 株式会社 ポリカーボネートの製造方法
JP2519996B2 (ja) * 1988-12-06 1996-07-31 ダイセル化学工業株式会社 難燃性オリゴカ―ボネ―トの製造法

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023118408A1 (en) 2021-12-24 2023-06-29 Avantium Knowledge Centre B.V. Process for the production of polyester copolymers

Also Published As

Publication number Publication date
JP2554775B2 (ja) 1996-11-13
EP0488182A3 (en) 1993-01-13
JPH04202221A (ja) 1992-07-23
US5322919A (en) 1994-06-21

Similar Documents

Publication Publication Date Title
US6747119B2 (en) Method and system for preparing a polycarbonate, copolymerization reagent and polycarbonate
EP1427770B1 (de) Verfahren zur herstellung von polycarbonat
EP0673959B1 (de) Verfahren zur Herstellung aromatischer Polycarbonate
JPH04175368A (ja) 芳香族系ポリカーボネートの製造方法
KR20050030890A (ko) 폴리카보네이트 수지에서 반응 부산물을 감소시키는 방법
EP0575810A2 (de) Polykarbonat und Verfahren zu seiner Herstellung
US6303735B1 (en) Polycarbonate production method
US6340738B2 (en) Continuous method for manufacturing polycarbonate
US5322919A (en) Process for producing a polycarbonate in inert solvent
JP2000186137A (ja) ポリカーボネート及び光学材料
WO2001077205A1 (en) Salts of aryl sulfonic acids as catalysts for the preparation of polycarbonates
JP3093315B2 (ja) ポリカーボネート組成物の製造方法
EP0708128B2 (de) Verfahren zur herstellung von polycarbonat
JPH05239331A (ja) ポリカーボネート系樹脂組成物の製造方法
US20030120025A1 (en) Process for the production of polycarbonate
JP3043828B2 (ja) ポリカーボネート組成物
JP2004525911A (ja) 粗製二価フェノール中の残留酸種の中和法
JP3334723B2 (ja) ポリカーボネートの製造方法
US20020128425A1 (en) Process for the production of polycarbonate
JP3302431B2 (ja) 芳香族ポリカーボネートの製造方法
JP3591551B2 (ja) ポリカーボネートの製造方法
JP4651149B2 (ja) ポリカーボネートの製造方法
JPH08134341A (ja) ポリカーボネート組成物およびその製造方法
JP3390621B2 (ja) 芳香族ポリカーボネート樹脂及びその製造方法
JP3160113B2 (ja) 芳香族ポリカーボネートの製造方法

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): BE CH DE FR GB IT LI NL SE

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

AK Designated contracting states

Kind code of ref document: A3

Designated state(s): BE CH DE FR GB IT LI NL SE

17P Request for examination filed

Effective date: 19930703

17Q First examination report despatched

Effective date: 19950529

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: IDEMITSU PETROCHEMICAL CO., LTD.

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN REFUSED

18R Application refused

Effective date: 19971012